Method and apparatus for two-phase heat exchange fluid distribution in plate-type heat exchangers

ABSTRACT

Method and apparatus for heat exchanging a gaseous fluid and a liquid fluid with a third heat exchange fluid by a plate-type heat exchanger in a manner permitting variations of the gaseous mass flow rate relative to the liquid mass flow rate without relative maldistribution of the two fluid phases within the heat exchanger passages. Between the plates within the heat exchanger core, the gaseous and liquid fluids are separately distributed across the width of the heat exchanger. Only after the gaseous and liquid fluids have been thus uniformly distributed within the passages are they combined and passed in heat exchange relation with the third heat exchange fluid. The problems associated with relative maldistribution of the two fluid phases which normally accompany conventional arrangements for distributing a two-phase fluid across the width of a plate-type heat exchanger are thus avoided. Four embodiments of the invention are described and shown.

United States Patent [72] Inventors James J. Schauls;

Franklin D. Duncan, La Crosse, Wis.

[21] Appl. No. 858,373

[22] Filed Sept. 16, 1969 [45] Patented Feb. 2, 1971 [73] Assignee The Trane Company La Crosse, Wis. a corporation of Wisconsin.

[54] METHOD AND APPARATUS FOR TWO-PHASE HEAT EXCHANGE FLUID DISTRIBUTION IN PLATE-TYPE HEAT EXCHANGERS 32 Claims, 23 Drawing Figs.

[52] U.S.Cl. 165/1,

[51] Int. Cl F28f 3/00 [50] Field of Search 159/16;

[56] References Cited 1 UNITED STATES PATENTS 3,073,380 H1963 Palmason 165/167X 3,282,334 11/ 1966 Stahlheber 165/1'66 3.488,686 l/l970 Dunwoodyetal ABSTRACT: Method and apparatus for heat exchanging a gaseous fluid and a liquid fluid with a third heat exchange fluid by a plate-type heat exchanger in a manner permitting variations of the gaseous mass flow rate relative to the liquid mass flow rate without relative maldistribution of the two fluid phases within the heat exchanger passages. Between the plates within the heat exchanger core, the gaseous and liquid fluids are separately distributed across the width of the heat exchanger. Only after the gaseous and liquid fluids have been thus uniformly distributed within the passages are they combined and passed in heat exchange relation with the third heat exchange fluid. The problems associated with relative maldistribution of the two fluid phases which normally accompany conventional arrangements for distributing a two-phase fluid across the width of a plate-type heat exchanger are thus avoided. Four embodiments of the invention are described and shown.

PATENTED FEB 2197:

saw a or 5 INVENTOR. JAMES J. SCHAULS FRANKLIN D. DUNCAN ATTORNEY PATENTEDFEB 2mm 3559.722

sum 5 OF 5 INVENTOR. JAMES J. SCHAULS FRANKLIN D. DUNCAN ATTORNEY METHOD AND APPARATUS FOR TWO-PHASE HEAT EXCHANGE FLUID DISTRIBUTION IN PLATE-TYPE HEAT EXCHANGERS BACKGROUND OF THE INVENTION In modern processes such as the separation of natural gas or air intotheir components, it often becomes necessary to heat exchangea two-phase fluid with another fluid. However, many attempts to pass a fluid consisting of a liquid and a gas into a heat exchanger have failed because of the relative maldistribution of the two phases. Certain of the passages or certain portions of the passages would conduct excess liquid while other passages or portions of passages would conduct excess gas. Ideally, the liquid and the gas should be uniformly distributed to obtain maximum heat exchange with the third or other heat exchange fluids. These problems have been partially solved by first separating the two-phase fluid into its constituent phases. Various heat exchanger designs such as those shown in U.S. Pat. Nos. 3,282,334 and 3,310,105 both assigned to the assignee of this invention, have been directed to the problem of distributing the liquid phase uniformly among the vapor-liquid passages and distributing the gaseous phase uniformly among the vapor-liquid passages whereby each of the passages intended to conduct a vapor and liquid mixture receive the proper proportion of vapor and liquid. However, in those heat exchanger designs the vapor and the liquid are mixed at the inlet to the vapor-liquid passage. This mixture must then be distributed within the passages across the width of the heat exchanger. To accomplish this, those heat exchanger designs utilized a distributor structure comprising a corrugated metallic sheet fin material the convolutions of which form flow paths which extend from the inlet to the full width of the heat exchanger passage. To further enhance the distribution of gas and liquid within the passage, a section of hardway" distributor fin consisting of a porous corrugated metallic sheet fin material having crests extending transversely to the direction of fluid flow, may be disposed within the passage. While this distributor structure has been partially successful, it should be appreciated that its affect upon a gaseous fluid will be somewhat different from its affect upon a liquid of substantially greater density and viscosity. This may result in a nonuniform distribution of liquid and gas across the width of the vapor-liquid passage. This is especially critical when the mass flow rate of either the liquid or the gas is varied. It is also critical when the attitude of the heat exchanger is such that the liquid does not flow downwardly through the heat exchange passage.

SUMMARY OF THE INVENTION This invention solves the aforementioned problems by providing an entirely different method and apparatus for distributing gas and liquid in the passages of a plate-type heat exchanger intended to conduct a mixture of both fluid phases. More particularly this invention provides a means of uniformly distributing both the vapor and the liquid phases among the several passages of a heat exchanger and additionally provides a means of uniformly distributing the vapor and liquid phases across the width of each of the several passages. Because of superior distribution of the liquid and gaseous phases, it is possible to orient the heat exchanger for either upflow or downflow of liquid and to vary the mass flow rate of either the gas or the liquid fluid over a wide range without substantial reduction in heat exchanger etficiency.

Specifically this invention relates to a method of heat exchanging a first heat exchange fluid with a gaseous phase heat exchange fluid and a liquid phase heat exchange fluid including the steps of: providing a first supply of liquid phase heat exchange fluid; providing a second supply of gaseous phase heat exchange fluid; providing a third supply of a third heat exchange fluid; introducing the fluid of one of said phases into a first layer of a multilayer heat exchanger; distributing said introduced fluid of said one phase within said first layer substantially uniformly across the width of said heat exchanger; introducing the fluid of the other of said phases into a second layer adjacent said first layer; distributing said introduced fluid of said other phase within said second layer substantially uniformly substantially across the width of said heat exchanger; transferring the substantially uniformly distributed fluid of one of said phases from one of the first and second layers and diffusing it into the substantially uniformly distributed fluid of the other phase from the other of the first and second layers while substantially maintaining its uniform distribution substantially across the width of said heat exchanger whereby the gaseous and liquid phases are substantially uniformly combined substantially across the width of a heat exchanger independently of their relative mass flow rates; and passing the substantially uniformly distributed combined gaseous and liquid phase heat exchange fluids in heat exchange relation with said third heat exchange fluid.

Specifically this invention further relates to a plate-type brazed heat exchanger comprising: first and second elongated metallic plates of generally similar peripheral configuration contraposed in face-to-face spaced relationship; first sealing means sealingly connecting said elongated metallic plates along the peripheral margins thereof thereby enclosing with said first and second elongated metallic plates a generally flat elongated plenum; a platelike partition interleaved with said first and second elongated metallic plates adjacent at least one end of said plenum and being coincidental with a plane spaced from said first and second elongated plates bisecting said plenum into first and second spacial layers; said partition extending transversely of the longitudinal axis of said elongated plenum to and in sealing connection with said first sealing means thereby defining within said first spacial layer a first passage intermediate said partition and said first elongated plate and within said second spacial layer a second passage intermediate said partition and said second elongated plate; said first sealing means defining a first inlet to said first passage adjacent said one end of said plenum for admitting one of a first gaseous phase and a second liquid phase heat exchange fluids; said first sealing means defining a second inlet to said second passage adjacent said one end of said plenum for admitting the other of said gaseous phase and liquid phase heat exchange fluids; said first sealing means further defining at the other end of said plenum a first outlet from said plenum; first distributor means in one of said first and second passages abutting one face of said partition for substantially uniformly distributing one of said first and second heat exchange fluids respectively from one of said first and second inlets within said one passage substantially across the width of said plenum; a transfer passage means within said plenum for combining said one uniformly distributed heat exchange fluid with the other of said first and second fluids; and means defining a third passage disposed in heat exchange relation with the combined first and second heat exchange fluids.

DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic of a gas separation system utilizing the heat exchange means of the instant invention.

FIG. 2 is a front elevation of a plate-type heat exchanger incorporating a first form of the invention.

FIG. 3 is a side elevation of the heat exchanger shown in FIG. 2.

FIG. 4 is a section taken at line 4-4 of FIG. 2.

FIG. 5 is a section taken at line 5-5 of FIG. 3.

FIG. 6 is a section taken at line 6-6 of FIG. 3.

FIG. 7 is a front elevation of a plate-type heat exchanger incorporating a second embodiment of the invention.

FIG. 8 is a side elevation of the heat exchanger shown in FIG. 7.

FIG. 9 is a section taken at line 9-9 of FIG. 7.

FIG. 10 is a section taken at line 10-10 of FIG. 8.

FIG. 1 1 is a section taken at line 1 1-1 1 of FIG. 8.

FIG. 12 is-a front elevation of a heat exchanger incorporating a third embodiment of the invention.

FIG. 13 is a side elevation of the heat exchanger shown in FIG. 12.

FIG. 14 is a section taken at line 14-14 of FIG. 12.

FIG. 15 is a section taken at line 15-15 of FIG. 14.

FIG. 16 is a section taken at line 16-16 of FIG. 14.

FIG. 17 is a partial section of the heat exchanger taken at line 17-17 ofFIG. 14.

FIG. 18 is a front elevation of a heat exchanger incorporating a fourth embodiment of the invention.

FIG. 19 is a side elevation of the heat exchanger shown in FIG. 18.

FIG. 20 is a vertical section of a portion of the heat exchanger taken along line 20-20 of FIG. 18.

FIG. 21 is a section taken along line 21-21 of FIG. 20.

FIG. 22 is a section taken along line 22-22 of FIG. 20.

FIG. 23 is a section of a portion of the heat exchanger taken along line 23-23 of FIG. 20.

DETAILED DESCRIPTION A first 1 shows an exemplary system utilizing a heat exchanger employing the instant invention. A gas feed such as air or natural gas under pressure is supplied to header 11. The gas feed (See distributed by header 11 to certain passages within the heat exchanger 10. The gas is cooled as it passes through these passages and a portion thereof is condensed. The liquid and gaseous portions are discharged from these passages to a header 12. The gas and liquid mixture is then conducted to a separator 13. The liquid portion from separator 13 may be throttled to a lower pressure by throttling means 14 with the resulting vapor liquid mixture being passed to separator 15. The gas from separator may be withdrawn from the system by way of a valve 16, or may be returned to the heat exchanger 10 via valve 17 and gas header 18 to recover its cold content. Likewise, the liquid fluid from separator 15 may be withdrawn from the system by way of valve 19 or alternatively returned to heat exchanger 10 via valve and liquid header 21. The gas from header l8 and the liquid from header 21 are separately distributed uniformly within the passages across the width of head exchanger 10. After being so distributed within the core of heat exchanger 10, the gas and liquid phase fluids are combined to form a twophase fluid which is passed in heat exchange relation with the feed gas, and is discharged from the heat exchanger core via discharge header 22.

The gas from separator 13 may be further separated into various constituents which may be in part or total returned through various passages (not shown) of heat exchanger 10 to recover their cold content. The relative proportions of liquid and gas returned to heat exchanger 10 via headers 21 and 18 can be varied by adjustments of valves 16, 17, 19 and 20. It will be appreciated that for purposes of practicing the invention herein disclosed, the liquid supplied to header 21 and the gas supplied to header 18 may be derived from sources other than the feed fluid. Furthermore, the feed fluid may enter the heat exchanger header 11 as a liquid, gas, or liquid and gas mixture.

Throughout the drawings of this disclosure heavy dashed vectors represent gas flow, heavy solid vectors represent liquid flow, and heavy dash-dot vectors represent the flow of a third heat exchange fluid which may be a liquid, gas, or liquid gas mixture.

Now referring to the embodiment of the invention shown in FIGS. 2-6 with particular attention to FIGS. 3 and 4, it will be seen that heat exchanger 10 has a core 23 comprised of a plurality of rectangular impervious metallic plates 24 of the same peripheral configuration contraposed in face-to-face parallel spaced relationship. Disposed within each of the plenums formed intermediate adjacent plates 24, is a metallic platelike partition 25 interleaved with, parallel to, and spaced from metallic plates 24. Each partition 25 has substantially the same peripheral configuration, although not shown, as plates 24. Each partition 25 separates the plenum between adjacent plates 24 into first and second spacial layers 26 and 27 respectively.

A first sealing means in he form of a series of closing bars 28 bridging between each partition 25 and the adjacent plates 24 along the peripheral margins thereof (See FIGS. 5 and 6) in each of the layers 26 and 27 bound the plenums between adjacent pairs of plates 24. Bars 28 are sealingly bonded to the margins of plates 24 and partitions 25 by brazing. It should be appreciated that the sealing effect of bars 28 may be obtained by elements of other configuration such as s channel members, rods, tubes, etc.

Now referring specifically to FIG. 5 where the full width of one of layers 26 and the details therein can be viewed, it will be seen that a gap is provided at the lower end of layer 26 between the ends of bars 28 to thereby define a gas inlet 29 to a first passage, and that a second gap is provided at the upper portion of layer 26 between the ends of the bars 28 to form a fluid outlet 30 from the first passage.

Disposed adjacent inlet 29 and outlet 30 is a substantially triangular section 31 of corrugated metallic sheet fin material having crests extending vertically. A trapezoidal section 32 of corrugated metallic sheet fin material is disposed laterally of each fin section 31 and has crest extending diagonally as shown to provide a flow pattern between the inlet or outlet and the full width of the heat exchanger. A small rectangular section 33 of corrugated metallic sheet fin material having crests extending horizontally is arranged immediately above the lower trapezoidal section 32. Section 33 must be porous as the gas passes the hard way therethrough and is accordingly tenned a hardway" fin section. Immediately below the upper fin section 32 is a large rectangular section 34 of corrugated metallic sheet fin material having crests extending vertically.

In the area intermediate fin section 34 and hardway section 33, the partition 25 is provided with a slit 35 which extends horizontally across the width of the heat exchanger 10. In FIG. 5, a portion of the fin sections has been removed to expose partition 25 and slit 35. As will be discussed hereinafter, slit 35 defines a transfer passage for the transfer of liquid fluid from a second passage within an adjoining layer 27 into the gas stream passing through the first passage in layer 26. Slit 35 may be formed simply by spacing two separate plates to form the partition 25. In the alternative slit 35 may be formed by cutting an elongated opening in a single piece partition. In either event, the ends of slit 35 may be formed adjacent the sides of heat exchanger 10 are closed to prevent external leakage. Since the plates within a plate-type heat exchanger constitute a structural element which is substantially weakened by an interruption such as slit 35, a rectangular section 36 of corrugated metallic heavy guage fin material having crests extending vertically is disposed within layer 26 overlying partition 25 at both sides of slit 35. Fin section 36 is brazed to partition 25"to provide the necessary structural continuity bridging slit 35. We therefore refer to this type fin as a bridging fin.

Gas entering inlet 29 as illustrated by the heavy dashed vectors in FIGS. 4 and 5 is distributed across the width of the heat exchanger via lower fin sections 31, 32 and 33 in the lower portion of the heat exchanger. After having been uniformly distributed across the width of the heat exchanger, the gas is mixed with liquid entering the first passage via transfer passage slit 35 as illustrated by the heavy solid vectors in FIGS. 4 and 5. The liquid and gaseous fluids respectively uniformly distributed across the width of the heat exchanger and subsequently combined in intimate contact with each other then flow upwardly through the main fin section 34 of the first passage. The fluid is then collected at the top of the heat exchanger and directed to the outlet 30 via upper fin sections 32 and 31 adjacent outlet 30 from whence it passes to header 22. l-lardway" fin 33 in addition to serving as part of the gas distributing means also serves to reduce liquid flooding of the gas header 18.

Now referring specifically the FIG. 6 showing one of layers 27, it will be seen that the ends of bars 28 in layer 27 are spaced one from the other to thereby define a liquid inlet 37 in the lower portion of the heat exchanger, a fluid inlet 38 in the upper portion of the heat exchanger, and a fluid outlet 39 in the lower portion of the heat exchanger. Inlets 37 and 38 and outlet 39 communicate respectively with headers 21, 11, and 12. The space within layer 27 is sealingly bisected into second and third passages by a second sealing means in the form of a horizontally extending bar 40 which bridges between partition 25 and plate 24 as best seen in FIGS. 4 and 6. The space within layer 27 above bar 40, i.e., the space of the third passage, is provided with first triangular sections 41 of corrugated metallic sheet fin material having crests extending horizontally, disposed adjacent inlet 38 and outlet 39. Second triangular sections 42 of corrugated metallic sheet fin material having crests extending vertically are disposed intermediate each of fin sections 41 and a large rectangular section 43 of corrugated metallic sheet fin material also having crests extending vertically. Fluid passing from header ll enters the third passage through inlet 38 and is distributed across the width of the heat exchanger via upper fin section 41 from whence it passes downwardly through upper triangular section 42, rectangular a section 43, and lower triangular section 42 where it is collected in lower fin section 41 and delivered from the third passage to header 12 via outlet 39. This flow of fluid in the third passage is illustrated by the heavy dash-dot vectors in FIGS. 4 and 6. The fluid is thus passed in counterfiow heat exchange relation with the fluid passing through the first passage in layer 26, the heat transfer taking place between layers 26 and 27 through metallic partition 25.

Within layer 27 below bar 40 is a first triangular section 44 of corrugated metallic sheet fin material having crests extending horizontally to inlet 37, and a second triangular section 45 of corrugated metallic sheet fin material having crests extending vertically. A rectangular section 46 of bridging fin similar to the bridging fin of section 36 is disposed immediately below bar 40 in layer 27 overlying and brazed to the area of partition 25 immediately adjacent slit 35. Section 46 like section 36 is constructed from heavy guage corrugated metallic sheet fin material having crests extending vertically to thereby provide structural continuity in the area of slit 35. Immediately below bridging fin 46 is a rectangular hardway fin section 47 of corrugated metallic sheet fin having crests extending horizontally. Like hardway section 33, hardway section 47 is porous to permit passage of fluid therethrough transversely of the crests thereof. In FIG. 6 a portion of the fin sections has been removed to expose partition 25 and slit 35. Liquid entering inlet 37 to the second passage from header 21 passes respectively through triangular section 44, triangular section 45, and hardway" section 47 and is thus uniformly distributed across the width of the heat exchanger in the second passage. After having been thus distributed across the width of the heat exchanger, the liquid fluid passes along the bridging fin and is transferred from layer 27 to layer 26 through the slit 35 as herein before described. This flow of liquid in the second passage is illustrated by the heavy solid vectors.

Thus it will be seen that a two-phase mixture fluid passing through the major portion of layers 26 is heat exchanged with the third fluid passing through layers 27. However, a portion of each layer 27 at the lower end thereof provides means for distributing liquid uniformly across the width of the heat exchanger prior to being transferred into the gaseous stream of layer 26. Since the gas is uniformly distributed across the width of the heat exchanger in layer 26, and the liquid is uniformly distributed across the width of the heat exchanger in layer 27 there is no necessity to further distribute these fluids across the width of the heat exchanger after they are combined even if the relative proportions of combined liquid and gas are varied as aforementioned. The flow vectors shown in FIG. 2 are a superimposed composite of the flow vectors of FIGS. 5 and 6 and illustrate the flow pattern for the aforedescribed heat exchange.

Now referring to the embodiment of the invention shown in FIGS. 7

be seen that heat exchanger 10a has a core 23 a comprised of a plurality of rectangular impervious metallic plates 24a of the same peripheral configuration contraposed in face-to-face parallel spaced relationship. Disposed within each of the plenums formed intermediate adjacent plates 24a, is a metallic platelike partition 25a interleaved with, parallel to, and spaced from metallic plates 240. Each partition 25a has substantially the same peripheral configuration, although not shown, as plates 24a. Each partition 25a separates the plenum between adjacent plates 24a into first and second spacial layers 26a and 27a respectively.

A first sealing means in the form of a series of closing bars 280 bridging between each partition 25a and the adjacent plates 24a along the peripheral margins thereof (See FIGS. 10 and 11) in each of the layers 26a and 27a bound the plenums between adjacent pairs of plates 24a. Bars 28a are sealingly bonded to the margins of plates 24a and partitions 250 by brazing. It should be appreciated that the sealing effect of bars 28a may be obtained by elements of other configuration such as channel members, rods, tubes, etc.

Now referring specifically to FIG. 10 where the full width of one of layers 26a and the details therein can be viewed, it will be seen that a gap is provided at the lower end of layer 260 between the ends of bars 28a to thereby define a liquid inlet 29a to a first passage, and that a second gap is provided at the upper portion of layer 26a between the ends of the bars 28a to form a fluid outlet 30a from the first passage.

Disposed adjacent inlet 29a and outlet 30a is a substantially triangular section 31a of corrugated metallic sheet fin material having crests extending vertically. A trapezoidal section 32a of corrugated metallic sheet fin material is disposed laterally of each fin section 31a having crests extending diagonally as shown to provide a flow pattern between the inlet or outlet and the full width of the heat exchanger. A small rectangular section 33a of corrugated metallic sheet fin material having crests extending horizontally is arranged immediately above the lower trapezoidal section 32a. Section 33a must be porous as the liquid passes the hard way therethrough and is accordingly termed a hardway" fin section. Immediately below the upper fin section 320 is a large rectangular section 34a of corrugated metallic sheet fin material having crests extending vertically.

In the area intermediate fin section 340 and hardway section 33a, the partition 25a is provided with a slit 35a which extends horizontally across the width of the heat exchanger 10a. In FIG. 10 a portion of the fin sections has been removed to expose partition 25a and slit 35a. As will be discussed hereinafter, slit 35a defines a transfer passage for the transfer of gaseous fluid from a second passage within an adjoining layer 27a into the liquid stream passing through the first passage in layer 26a. Slit 35a may be formed simply by spacing two separate plates to form the partition 25a. In the alternative slit 35a may be formed by cutting an elongated opening in a single piece partition. In either event, the ,ends of slit 35a adjacent the sides of heat exchanger 10a are closed to prevent external leakage. Since the plates within a plate-type heat exchanger constitute a structural element which is substantially weakened by an interruption such as slit 35a, a rectangular section 36a of corrugated metallic heavy guage sheet fin material having crests extending vertically is disposed within layer 26a overlying partition 25a at both sides of slit 35a. Fin section 36a is brazed to partition 25a to provide the necessary structural continuity bridging slit 350. We therefore refer to this type fin as a bridging fin.

Liquid entering inlet 29a to the first passage from header 21a as illustrated by the heavy solid vectors in FIGS. 9 and 10 is distributed across the width of the heat exchanger via lower fin sections 31a and 32a and 33a in the lower portion of the heat exchanger. After having been uniformly distributed across the width of the heat exchanger, the liquid is mixed with gas entering the first passage via transfer passage slit 35a as illustrated by the heavy clashed vectors in FIGS. 9 and 10.

--ll with particular attention to FIGS. Sand 9, it will 5- The liquid and gaseous fluids respectively unifomily distributed across the width of the heat exchanger and subsequently combined in intimate contact with each other then flow upwardly through the main fin section 34a of the first passage. The fluid is then collected at the top of the heat exchanger and directed to the outlet 30a via upper fin sections 32a and 31a adjacent outlet 300 from whence it passes to header 220.

Now referring specifically to FIG. 11 showing layer 27a, it will be seen that the ends of bars 28a in layer 27a are spaced one from the other to thereby define a gas inlet 37a at the lower portion of the heat exchanger, a fluid inlet 38a in the upper portion of the heat exchanger, and a fluid outlet 39a in the lower portion of the heat exchanger. Inlets 37a and 38a and outlet 39a communicate respectively with headers 18a, Ila and 12a. The space within layer 27a is sealingly bisected into second and third passages by a second sealing means in the form of a horizontally extending bar 40a which bridges between partition 25a and plate 240 as best seen in FIGS. 9 and 11. The space within layer 27a above bar 400, i.e.. the space of the third passage, is provided with first triangular sections 41a of corrugated metallic sheet fin material having crests extending horizontally, disposed adjacent inlet 38a and outlet 39a. A second triangular section 42a of corrugated metallic sheet fin material having crests extending vertically is disposed intermediate each of fin sections 41a and a large rectangular section 43a of corrugated metallic sheet fin material also having crests extending vertically. Fluid passing from header 11a enters the third passage through inlet 38a and is distributed across the width of the heat exchanger via upper fin section 41a, from whence it passes downwardly through upper triangular section 424, rectangular section 43a, and lower triangular section 42a where it is collected in lower fin section 41:: and delivered from the third passage to header 120 via outlet 390. This flow of fluid in the third passage is illustrated by the heavy dash-dot vectors in FIGS. 9 and 11. The fluid is thus passed in head exchange relation with the fluid passing through the first passage in layer 26a, the heat transfer taking place between layers 26a and 27a through metallic partition 25a.

Within layer 27a below bar 40a is a first triangular section 44a of corrugated metallic sheet fin material having crests extending horizontally to inlet 37a, and a second triangular section 450 of corrugated metallic sheet fin material having crests extending vertically. Immediately below triangular section 450 is a rectangular hardway fin section 47a of corrugated metallic sheet fin having crests extending horizontally. Like hardway" 33a, hardway section 47a is porous to permit passage of gas therethrough transversely of the crests thereof. A rectangular section 460 of bridging fin similar to bridging fin 36a is disposed immediately below hardway" section 47a in layer 27a overlying and brazed to the area of separator 25:: immediately adjacent slit 350. Section 46a like section 36a is constructed from a heavy sheet of corrugated sheet fin material having crests extending vertically to thereby provide structural continuity in the area of slit 35a. In FIG. 11 a portion of the fin sections has been removed to expose partition 25a and slit 350.

Gas entering inlet 37a to the second passage from header 18a passes respectively through triangular section 440, downwardly through triangular section 45a, and hardway section 47a and is thus uniformly distributed across the width of the heat exchanger in the second passage. After having been thus distributed across the width of the heat exchanger, the gas passes along the bridging fin 460' and is transferred from layer 27a to layer 26a through the slit 35a as herein before described. This flow of gas in the second passage is illustrated by the heavy dashed vectors.

Thus it will be seen that a two-phase mixture fluid passing through the major portion of layers 26a is heat exchanged with the third fluid passing through the layers 274. However, a portion of each layer 270 at the lower end thereof provides means for distributing gas across the width of the heat exchanger prior to being transferred into the liquid stream of layer 26a.

Since the liquid is uniformly distributed across the width of the heat exchanger in layer 26a, and the gas is uniformly distributed across the width of the heat exchanger in layer 27a, there is no necessity to further distribute these fluids across the width of the heat exchanger after they are combined even if the relative proportions of combined liquid and gas are varied as aforementioned. The flow Vectors shown in FIG. 7 are a superimposed composite of the flow vectors of FIGS. 10 and 11 and illustrate the flow pattern for the aforedescribed heat exchange. It should be noted that in the embodiment of FIGS. 7 through 11, it is the gas stream that passes through the transfer passage slit 35a in the partition 25a. Since the gas inlet 37a is disposed vertically intermediate bar 40a and slit 35a, the gas is first caused to pass downwardly in layer 27a before passing upwardly in layer 26a. The downward course of the gas flow in layer 27a provides an effective means of preventing liquid under low flow conditions from backing up into the gas supply.

Now referring to the embodiment of the invention shown in FIGS. l2l7 with particular attention to FIGS. 13 and 14, it will be seen that heat exchanger 10b has a core 23b comprised of a plurality of rectangular impervious metallic plates 24b of the same peripheral configuration contraposed in face-to-face parallel spaced relationship. Disposed within the lower portion-of each of the plenums formed intermediate certain pairs of adjacent plates 24b, is a rectangular metallic platelike partition 25b interleaved with, parallel to, and spaced from metallic plates 24b. Partitions 24b have a vertical extent as shown in FIG. 14 and a horizontal extent equal to plates 24b. A portion of the fin material has been removed in FIG. 16 to directly expose a portion of the face of one of partitions 25b. Each partition 25b separates the lower portion of its respective plenum into first and second spacial layers 26b and 27b respectively.

A series of closing bars 28b sealingly bridging between each partition 25b and the adjacent plates 24b along the margins thereof at the lower portion of plates 24b in each of the layers 26b and 27b and between adjacent plates 24b along the margins thereof at the upper portion of plates 24b bound the plenums between said certain pairs of adjacent plates 24b. Bars 281; are sealingly bonded to the margins of plates 24b and partitions 25b by brazing. It should be appreciated that the sealing effect of bars 28b may be obtained by elements of other configurations such as channel members, rods, tubes, and etc.

Now referring specifically to FIG. 16 where the full width of one of layers 26b and the details herein can be viewed, it will be seen that a gap is provided at the lower end of layer 26b between the ends of bars 28b to thereby define a gas inlet 29b to a first passage, and that a second gap is provided at the upper portion of said plenum between the ends of bars 28b to form a fluid outlet 30b from the first passage.

Disposed adjacent inlet 29b and outlet 30b is a substantially triangular section 31b of corrugated metallic sheet fin material having crests extending vertically. Disposed adjacent outlet 30b is a substantially triangular section of corrugated sheet fin 31b having its crests extending vertically. A trapezoidal section 32b of corrugated metallic sheet fin material is disposed laterally of fin section 31b having crests extending diagonally as shown to provide a flow pattern from inlet 29b to the full width of the heat exchanger. A trapezoidal section 32b of corrugated metallic sheet fin material is disposed laterally of fin section 31b having crests extending diagonally as shown to provide a flow pattern from the full width of the heat exchanger to outlet 30b. A small rectangular section 33b of corrugated metallicsheet fin material having its crests extending horizontally is arranged immediately above trapezoidal section 32b. Section 33b must be porous as the fluid passes the hardway therethrough and'is accordingly termed a hardway" fin section. Intermediate hardway fin section 33b and trapezoidal fin section 32b is a large rectangular section 34b of corrugated metallic sheet fin material having its crests extending vertically. It should be noted that fin sections 31b, 32b and 34b are sufficiently thick as to bridge between spaced plates 24b whereas fin sections 33b, 31b and 32b are sufi'iciently thick as to bridge only between a plate 24b and a partition 25b.

Gas entering inlet 29b from header 18b as illustrated by the heavy dashed vectors in FIGS. 14 and 16 is distributed across the width of the heat exchanger via lower fin sections 31b, 32b, and 33b. After the gas has been completely distributed across the width of the heat exchanger by passing through fin sections 31b, 32b, and 33b, it passes beyond the upper edge of partition 25b into fin section 34b where it is combined with liquid, as illustrated by the heavy solid vectors in FIGS. 14, 16, and 17, entering the fin section 34b in a manner hereinafter described in connection with layer 26b. The liquid and gaseous fluids respectively uniformly distributed across the width of the heat exchanger and subsequently combined in intimate contact with each other then flow upwardly through the main fin section 34b of the first passage. The fluid is then collected at the top of the heat exchanger and directed to the outlet 30b via upper fin sections 32b and 31b adjacent outlet 30b from whence it passes to header 22b.

Now referring specifically to FIG. 17 showing one of layers 27b, it will be seen that the ends of bars 28b in layer 27b are spaced one from the other to thereby define a liquid inlet 37b, to a second passage which communicates with header 21b of heat exchanger b. Disposed within each layer 27b adjacent an inlet 37b is a first triangular section 44b of corrugated metallic sheet fin material having crests extending horizontally. A second triangular section 45b of corrugated metallic sheet fin material is disposed immediately above section 44b also having crests extending vertically. Immediately above fin section 45b is a rectangular hardway section 47b of corrugated metallic sheet fin material having crests extending horizontally. Like hardway" section 33b, hardway section 47b is porous to permit passage of fluid therethrough transversely of the crests thereof. Liquid entering inlet 37b from header 21b passes respectively through triangular section 44 b, triangular section 45b, and hardway" section 47b and is thus uniformly. distributed across the width of the heat exchanger in the second passage. After thus being distributed across the width of the heat exchanger, the liquid fluid passes vertically beyond the upper edge of partition 25b where it intimately mixes with the gas within fin section 34b of the first passage. In this particular embodiment of the invention it will be noted that no discrete slit or gap is provided within partition 25b. However, a transfer passage is formed as both layers 26b and 27b become a common layer above the upper edge of partition 25b.

It will be seen that the gas flowing within the first passage of layer 26b and the liquid flowing within the second passage of layer 27b are separately substantially uniformly distributed across the width of the heat exchanger prior to their combination, and that there is no necessity for further distribution of these fluids across the width of the heat exchanger after being so combined. The combined fluids flowing in section 34b, i.e., the upper portion of the first passage, are heat exchanged with a third heat exchange fluid flowing in a third passage of an ad jacent layer 50b as illustrated by the heavy dot-dash vectors of FIG. 15.

Referring now specifically to FIG. 15, the third passage is formed by certain other adjacent metallic plates 24b and closing bars 28b bridging therebetween along the margins thereof. It will be seen that the ends of bars 28b within layer 50b are spaced to define a fluid inlet 38b at the upper portion of the heat exchanger and a fluid outlet 39b at the lower portion of the heat exchanger arranged to communicate respectively with headers 11b and 12b. Disposed within the space of layer 50b adjacent each inlet 38b and outlet 39b is a substantially triangular section 41b of corrugated metallic sheet fin material having crests extending vertically. A trapezoidal section 42b of corrugated metallic sheet fin material is disposed laterally of each of fin sections 41b and has crests extending diagonally as shown to provide a flow pattern between the inlet or outlet and the full width of the heat exchanger. Intermediate trapezoidal sections 42b is a large rectangular section 43b of corrugated metallic sheet fin material which forms the main packing for the third passage within layer 50b. The fluid to be heat exchanged with the aforementioned gaseous and liquid fluids enters the third passage via header 1 lb, inlet38b and is distributed across the width of the heat exchanger by upper triangular section 41b and upper trapezoidal section 42b whereupon it moves downwardly through rectangular section 43b from which it is directed via lower trapezoidal section 42b and lower triangular section 41b to outlet 39b into header 12b.

Thus it will be seen that two-phase mixture fluid passing through the first passages is heat exchanged via plates 24b with the third fluid passing through the third passage within layer 50b. However, means is provided intermediate plates 24b for independent distribution of both the liquid and gaseous phases uniformly across the full width of the heat exchanger prior to their mixture. Since the gas is uniformly distributed across the width of the heat exchanger in layer 26b, and the liquid is uniformly distributed across the width of the heat exchanger in layer 27b there is no necessity to further distribute these fluids across the width of the heat exchanger after they are combined even if the relative proportions of combined liquid and gas varied as aforementioned. The flow vectors shown in FIG. 12 are a superimposed composite of the flow vectors of FIGS. 15, 16, and I7 and illustrate the flow pattern for the aforedescribed heat exchange.

Now referring to the embodiment of the invention shown in F IGS. 18-23 with particular attention to FIGS. 19 and 20, it will be seen that heat exchanger 10c has a core 230 comprised of a plurality of rectangular impervious metallic plates 24c of the same peripheral configuration contraposed in face-to-face parallel spaced relationship. Disposed within each of the plenums formed intermediate certain adjacent plates 24c, is a pair of rectangular metallic platelike partitions 25c interleaved with, parallel to, and spaced from the lower portions of metallic plates 240. Intermediate the planes of adjacent partitions 25c immediately above partitions 250 is a third rectangular metallic platelike partition 25c interleaved with, parallel to, and spaced from the upper portions of said certain plates 24c. Partition 250 has a vertical extent as shown in FIG. 20 and a horizontal extent equal to that of plates 24c. Portions of the fin material have been removed in FIGS. 22 and 23 to directly expose portions of the faces of partitions 25c and 250'. Each pair of partitions 25c separates the lower portion of the plenum between said certain adjacent plates 24c into a pair of spaced spacial layers 26c and an intermediate spacial layer 270 shown in FIGS. 22 and 23 respectively. Each partition 25c separates the upper portion of the plenum between said certain adjacent plates 24c into two identical spacial layers 260' shown in FIGS. 20 and 22. Each layer 26c is somewhat narrower than but coextensive and in fluid communication with a layer 26c. Layer 26c may be considered as a thickened extension of layer 260. Layer 27c is coextensive and in communication with two adjacent layers 26c. A series of closing bars 280 sealingly bridging between each partition 25c and the lower portion of adjacent plates 24c along the margins thereof in each of layers 26c, between partitions 250' along the lower and side margins thereof in layer 27c, bound each plenum between said certain adjacent pairs of plates 24c. Bars 270 are sealingly bonded to the margins of plates 24c and partitions 25c and 250 by brazing. It should be appreciated that the sealing effect of bars 280 may be obtained by elements of other configurations such as channel members, rods, tubes, etc.

Now referring specifically to FIG. 22 where the details of layers 26c and 260 are shown, it will be seen that a gap is provided between the ends of bars 280 at the lower end of the layer 26c to thereby define a gaseous fluid inlet 29c to a first passage, and that a second gap is provided between the ends of bars 28c at the upper portion of the first passage in layer 261: to form a fluid outlet 30c from said first passage. Disposed adjacent inlet 29c is a substantially triangular section 31c of corrugated metallic sheet fin material having crests extending vertically. Disposed adjacent outlet 30c is a substantially triangular section 31c of corrugated metallic sheet fin material having crests extending vertically. A trapezoidal section 32c of corrugated metallic sheet fin material is disposed laterally of fin section 3Ic having crests extending diagonally as shown to provide a flow pattern from inlet 29c to the full width of the heat exchanger. A trapezoidal section 32c of corrugated metallic sheet fin material is disposed laterally of fin section 31c having the crests extending diagonally as shown to provide a flow pattern from the full width of the heat exchanger to outlet 30c. A small rectangular section 33c of corrugated metallic sheet fin material having crests extending horizontally is arranged immediately about trapezoidal section 320. Section 33c must be porous as the gas passes the hard way therethrough and is accordingly termed a hardway fin section. Intermediate hardway fin section 33c and the trapezoidal fin section 32c is a large rectangular section 34c of corrugated metallic sheet fin material having crests extending vertically. It should be noted that the fin sections 31c, 32c and 34c are sufficiently thick as to bridge between a partition 25c and the adjacent plate 240 and that fin sections 31c, 32c, and 330 are sufiiciently thick as to bridge between partition 25c and adjacent plate 24c.

Gas entering inlet 290 from header 180 as illustrated by the heavy dashed vectors in FIGS. 20, 22 and 23, is distributed uniformly across the width of the heat exchanger via lower fin sections 310, 32c and 33c in the lower portion of the heat exchanger core 230. After the gas has been completely distributed across the width of the heat exchanger by passing through fin sections 31c, 32c and 33c, it passes beyond the upper edge of partition 25c into fin section 34cwhere it is combined with liquid as illustrated by the heavy solid vectors in FIGS. 20, 22 and 23 entering the fin section 34c in a manner hereinafter described in connection with layer 27c. The liquid and gaseous fluids respectively uniformly distributed across the width of the heat exchanger and subsequently combined in intimate contact with each other then flow upwardly through the main fin section 34c. The fluid is then collected at the top of the heat exchanger and directed to the outlet 300 via upper fin sections 32c and 31c adjacent outlet 300 from whence it passes to header 220.

Now referring specifically to FIG. 23 showing layer 27c, it will be seen that the ends of bars 280 of layer 270 are spaced one from the other to thereby define a liquid inlet 37c to a second passage which communicates with header 21c of heat exchanger c. Disposed within each layer 27c adjacent inlet 370 is a first triangular section 440 of corrugated metallic sheet fin material having crests extending horizontally. A second triangular section 45c of corrugated metallic sheet fin material is disposed immediately above section 44c having crests extending vertically. Immediately above fin section 45c is a rectangular hardway" section 47c of corrugated metallic sheet fin material having crests extending horizontally. Like hardway section 330, hardwayi' section 47c is porous to permit passage of liquid therethrough transversely of the crests thereof. Liquid entering inlet 37c to the second passage from header 21c passes respectively through triangular section 44c, triangular section 45c, and "hardway section 47c and is thus uniformly distributed across the width of the heat exchanger. After thus being distributed across the width of the heat exchanger in the second passage, the liquid fluid passes vertically beyond the upper edge of partition 250 where the liquid intimately mixes with the gaseous fluid in the first passage at fin sections 34c aforedescribed. In this particular embodiment of the invention it will be noted that no discrete slit or gap is provided within partition 25c. However, a transfer passage is formed as both layers 26c and 27c become a common layer 26c above the upper edge of partition 25c. It will be seen that the gas flowing within layer 26c and the liquid flowing within layer 27c are separately substantially uniformly distributed across the width of the heat exchanger prior to their combination, and that there is no necessity for further distribution of these fluids across the width of the heat exchanger after being so combined. The combined fluids flowing in section 34c, i.e., the upper portion of the first passage, are heat exchanged with a third heat exchange fluid flowing in a third passage of an adjacent layer 500 via plates 24c as illustrated by the heavy dot-dash vectors of FIG. 21. I

Referring now specifically to FIG. 21, the third passage is formed by certain other adjacent metallic plates 24c and closing bars 28c bridging therebetween along the margins thereof. It will be seen that the ends of bars 28c within layer 50c are spaced to define a fluid inlet 38c at the upper portion of the heat exchanger and a fluid outlet 39c at the lower portion of the heat exchanger arranged to communicate respectively with headers 11c and 12c. Disposed within the space of layer 50c adjacent inlet 38c and outlet 390 is a substantially triangular section 41c of corrugated metallic sheet fin material having crests extending vertically. A trapezoidal section 42c of corrugated metallic sheet fin material is disposed laterally of each of fin sections 41c and has crests extending diagonally as shown to provide a flow pattern between the inlet or outlet and the full width of the heat exchanger. Intermediate trapezoidal sections 42c is a large rectangular section 43c of corrugated metallic sheet fin material which forms the main packing for layer 50c. The third fluid to be heat exchanged with the aforementioned gaseous and liquid fluids enters the third passage in layer 50c via the header 1 1c, inlet 38c and is distributed as illustrated by the dot-dash vectors in FIG. 21 across the width of the heat exchanger by upper triangular section 41c and upper trapezoidal section 42c whereupon it moves downwardly through rectangular section 430 from which it is directed via lower trapezoidal section 42c and lower triangular section 41c to outlet 39c from the third passage into header 12c.

Thus it will be seen that two-phase mixture fluid passing through the first passage is heat exchanged with the third fluid passing through the third passage within layer 500 via plates 24c. However, means is provided between plates 24c for independent distribution of both the liquid and gaseous phases uniformly across the full width of the heat exchanger prior to their mixture.

Since the gas is uniformly distributed across the width of the heat exchanger in layer 26c, and the liquid is uniformly distributed across the width of the heat exchanger in layer 27c, there is no necessity to further distribute these fluids across the width of the heat exchanger after they are combined even if the relative proportions of the combined liquid and gas varied as aforementioned. The flow vectors shown in FIG. 18 are a superimposed composite of the flow vectors of FIGS. 21, 22 and 23 and illustrate the flow pattern for the aforedescribed heat exchange.

Reference may be made to FIGS. 9, 10 and 11 of U.S. Pat. No. 3,282,334 for a more comprehensive illustration of the types of material utilized in the corrugated metallic sheet fin sections for the heat exchanger embodiments disclosed herein.

In applying the second, third and fourth embodiments of the invention to the'system of FIG. 1, numerals 11, 12, 18, 21, and 22 will become respectively: 110, 12a, 18a, 21a, and 22a; 11b, 12b, 18b, 21b, and 22b, and 110, 12c, 18c, 21c, and 220. Their operation within the system of FIG. 1 is similar to that of the first embodiment.

We claim:

1. A plate-type heatexchanger apparatus comprising: first and second elongated metallic plates of generally similar peripheral configuration contraposed in face-to-face spaced relationship; first sealing means sealingly connecting said elongated metallic plates along the peripheral margins thereof thereby enclosing with said first and second elongated metallic plates a generally flat elongated plenum; a platelike partition interleaved with said first and second elongated metallic plates adjacent at least one end of said plenum and being generally coincident with a plane spaced from said first and second elongated metallic plates bisecting said plenum at said one end into first and second spacial layers; said partition extending transversely of the longitudinal axis of said elongated plenum substantially to said first sealing means thereby defining within one of said spacial layers a first passage intermediate said partition and said first elongated metallic plate and within the other of said spacial layer a second a passage intermediate said partition and said second elongated plate; said first sealing means defining a first inlet to said first passage adjacent said one end of said plenum for admitting one of a first gaseous phase and a second liquid phase heat exchange fluids; said first sealing means defining a second inlet to said second passage adjacent said one end of said plenum for admitting the other of said gaseous phase and liquid phase heat exchange fluids; said first sealing means further defining at the other end of said plenum a first outlet from said plenum; first distributor means in one of said first and second passages abutting one face of said partition for substantially uniformly distributing one of said first and second heat exchange fluids respectively from one of said first and second inlets within said one passage substantially across the width of said plenum; a transfer passage means within said plenum for combining said one uniformly distributed heat exchange fluid with the other of said first and second fluids, and means defining a third passage disposed in heat exchange relation with the combined first and second heat exchange fluids.

2. The apparatus as defined by claim 1 including a second distributor means in the other of said first and second passages abutting the other face of said partition for substantially uniformly distributing the other of said first and second heat exchange fluids respectively from the other of said first and second inlets within said other passage substantially across the width of said plenum.

3. The apparatus as defined by claim 2 wherein the sum of the thicknesses of said first distributor means, said second distributor means, and said partition substantially equal the thickness of said plenum.

4. The apparatus as defined by claim 1 wherein said distributor means includes a corrugated metallic sheet.

5. The apparatus as defined by claim 4 wherein the crest of said corrugated metallic sheet extended transversely of the longitudinal axis of said plenum and wherein said metallic sheet is perforated.

6. The apparatus as defined by claim 1 wherein said third passage is disposed within said second spacial layer and wherein said partition has approximately the same length as said first and second elongated metallic plates whereby said third passage is separated from said first spacial layer; and second sealing means disposed within said second spacial layer extending transversely of the longitudinal axis of said plenum for sealing separating said second passage from said third passage.

7. The apparatus as defined by claim 6 wherein said transfer passage is disposed intermediate said second inlet and said second sealing means with respect to said longitudinal axis.

8. The apparatus as defined by claim 6 wherein said second inlet is disposed intennediate said u'ansfer-passage and said second sealing means with respect to said longitudinal axis.

9. The apparatus as defined by claim 1 wherein said transfer passage extends through said partition.

10. The apparatus as defined by claim 9 wherein said transfer passage is substantially the full width of said plenum.

11. The apparatus as defined by claim 10 wherein said partition is comprised of two metallic plates disposed in end-to-end spaced relationship wherein the space therebetween defined defines said transfer passage.

12 The apparatus as defined by claim 9 wherein the longitudinal axis of said plenum is vertical; and wherein said transfer passage is disposed in the lower portion of said partition.

13. The apparatus as defined by claim 12 wherein said second inlet to said second passage is s disposed below said transfer passage.

14. The apparatus as defined by claim 12 wherein said inlet to said second passage is disposed above said transfer passage.

15. The apparatus as defined by claim 1 including a third elongated metallic plate of generally similar peripheral configuration to said first and second elongated metallic plates contraposed in face-to-face spaced relationship with said second elongated metallic plate externally of said plenum; said first sealing means further sealingly connecting said second and third elongated metallic plates along the peripheral margins thereof whereby said third passage is defined therebetween; said first sealing means defining an inlet and an outlet respectively to and from said third passage.

16. The apparatus as defined by claim 15 including a second partition within said plenum interleaved with said first partition and second elongated metallic plate whereby the opposing faces of said second passage are defined by said first and second partitions.

17. A method of heat exchange including the steps of: providing a supply of gaseous phase heat exchange fluid; providing a supply of liquid phase heat exchange fluid; introducing the fluid of one of said phases into a first layer of a multilayer heat exchanger; distributing said introduced fluid of said one phase within said first layer substantially uniformly substantially across the width of said heat exchanger; passing the substantially uniformly distributed fluid of said one phase through the remainder of said first layer; simultaneously introducing the fluid of the other of said phases into a second layer adjacent said first layer; distributing said introduced fluid of said other phase within said second layer substantially uniformly substantially across the width of said heat exchanger; and transferring the substantially uniformly distributed fluid of said other phase from said second layer to said first layer while substantially maintaining its uniform distribution substantially across the width of said heat exchanger whereby the gaseous and liquid phases are substantially uniformly combined substantially across the width of a heat exchanger independently of their relative mass flows.

18. A method of heat exchanging a first heat exchange fluid with a gaseous phase heat exchange fluid and liquid phase heat exchange fluid including the steps of: providing a first supply of liquid phase heat exchange fluid; providing a second supply of gaseous phase heat exchange fluid; providing a third supply of a third heat exchange fluid; introducing the fluid of one of said phases into a first layer of a multilayer heat exchanger; distributing said introduced fluid of said one phase within said first layer substantially uniformly substantially across the width of said heat exchanger; introducing the fluid of the other of said phases into a second layer adjacent said first layer; distributing said introduced fluid of said other phase within said second layer substantially uniformly substantially across the width of said heat exchanger; transferring the substantially uniformly distributed fluid of one of said phases from one of the first and second layers and diffusing it into the substantially uniformly distributed fluid of the other phase from the other of the first and second layers while substantially maintaining its uniform distribution substantially across the width of said heat exchanger whereby the gaseous and liquid phases a are substantially uniformly combined substantially across the width of a heat exchanger independently of their relative mass flow rates; and passing the substantially uniformly distributed combined gaseous and liquid phase heat exchange fluids in heat exchange relation with said third heat exchange fluid.

19. A method as defined by claim 18 wherein said one phase is the gaseous phase and said other phase is the liquid phase.

20. A method as defined by claim 18 wherein said one phase is the liquid phase and said other phase is the gaseous phase.

21. A method as defined by claim 18 wherein the combined gaseous and liquid phase fluids are passed generally upwardly through said other of said first and second layers.

22. A method of operating a plate-type heat exchanger having a plurality of substantially parallel spaced plates defining therebetween a plurality of relatively thin but wide passages including the steps of: passing a gas into a first of said relatively thin but wide passages formed by said plates; spreading said gas out in said first passage over substantially the full width of said plates forming said first passage; passing a liquid into a second of said relatively thin but wide passages formed by said plates; spreading said liquid out in said second passage over substantially the full width of said plates forming said second pasage; passing the thus spread gaseous and liquid fluids in substantially a common direction within their respective passages and passing one of said gaseous and liquid fluids beyond an edge of one of said plates forming one of a said first and second passages into the other of said gaseous and liquid fluids in the other of said passages for uniform intimate mixing of the gaseous and liquid fluids across the full width of said other passage; and passing the resulting mixture of gas and liquid in heat exchange relation via one of said plates with a third heat exchange fluid.

23. A method of operating a plate-type heat exchanger having a plurality of substantially parallel spaced plates defining therebetween a plurality of relatively thin but wide passages including the steps of: passing a gas into a first of said relatively thin but wide passages formed by said plates; spreading said gas out in said first passage over substantially the full width of said plates forming said first passage; passing a liquid into a second of said relatively thin but wide passages formed by said plates; spreading a said liquid out in said second passage over substantially the full width of said plates forming said second pasage; passing the thus spread gaseous and liquid fluids in substantially opposite directions within their respective passages and passing one of said gaseous and liquid fluids beyond an edge of one of said plates forming one of said first and second passages into the other of said gaseous and liquid fluids in the other of said'passages for uniform intimate mixing of the gaseous and liquid fluids across the full width of said other passage; and passing the resulting mixture of gas and liquid in heat exchange relation via one of said plates with a third heat exchange fluid.

24. A plate-type heat exchanger comprising: a plurality of substantially parallel closely spaced plates defining therebetween a plurality of relatively thin but wide passages;

one of said plates being common to a first and second passage adjacent to each other; said one plate having an edge in fluid communication with each of said first and second passages; said first passage having a gas inlet; means within said first passage downstream of said edge for distributing gas entering said gas inlet uniformly across the width of said first passage; said second passage having a liquid inlet; means within, said second passage downstream of said edge for distributing liquid entering said liquid inlet uniformly across the width of said second passage whereby said gaseous and liquid fluids are uniformly mixed as they pass beyond said edge of said one plate; and a third passage for conducting a third heat exchange fluid in heat exchange relation with the mixture of gas and liquid fluids.

25 The apparatus as defined by claim 24 wherein said edge extends transversely to said first passage.

26. The apparatus as defined by claim 24 wherein said edge extends substantially across the full width of said first and second passages.

27. The apparatus as defined by claim 24 wherein said edge is lower than said gas inlet to a said first passage.

28. The apparatus as defined by claim 24 wherein said gas distributing means and said liquid distributing means abut opposite faces of said one plate.

29. The apparatus as defined by claim 24 wherein said edge is the peripheral edge of said plate.

30. The apparatus as defined by claim 29 including a second plate having a peripheral edge parallel to and spaced from said first edge, the space between said edges conducting one of said gaseous and liquid fluids into the other of said gaseous and liquid fluids.

31. The apparatus ad as defined by claim 30 wherein said one plate and said second plate are coplanar.

32. The apparatus as defined by claim 29 wherein said one plate and said second plate are noncoplanar. 

1. A plate-type heat exchanger apparatus comprising: first and second elongated metallic plates of generally similar peripheral configuration contraposed in face-to-face spaced relationship; first sealing means sealingly connecting said elongated metallic plates along the peripheral margins thereof thereby enclosing with said first and second elongated metallic plates a generally flat elongated plenum; a platelike partition interleaved with said first and second elongated metallic plates adjacent at least one end of said plenum aNd being generally coincident with a plane spaced from said first and second elongated metallic plates bisecting said plenum at said one end into first and second spacial layers; said partition extending transversely of the longitudinal axis of said elongated plenum substantially to said first sealing means thereby defining within one of said spacial layers a first passage intermediate said partition and said first elongated metallic plate and within the other of said spacial layer a second a passage intermediate said partition and said second elongated plate; said first sealing means defining a first inlet to said first passage adjacent said one end of said plenum for admitting one of a first gaseous phase and a second liquid phase heat exchange fluids; said first sealing means defining a second inlet to said second passage adjacent said one end of said plenum for admitting the other of said gaseous phase and liquid phase heat exchange fluids; said first sealing means further defining at the other end of said plenum a first outlet from said plenum; first distributor means in one of said first and second passages abutting one face of said partition for substantially uniformly distributing one of said first and second heat exchange fluids respectively from one of said first and second inlets within said one passage substantially across the width of said plenum; a transfer passage means within said plenum for combining said one uniformly distributed heat exchange fluid with the other of said first and second fluids, and means defining a third passage disposed in heat exchange relation with the combined first and second heat exchange fluids.
 2. The apparatus as defined by claim 1 including a second distributor means in the other of said first and second passages abutting the other face of said partition for substantially uniformly distributing the other of said first and second heat exchange fluids respectively from the other of said first and second inlets within said other passage substantially across the width of said plenum.
 3. The apparatus as defined by claim 2 wherein the sum of the thicknesses of said first distributor means, said second distributor means, and said partition substantially equal the thickness of said plenum.
 4. The apparatus as defined by claim 1 wherein said distributor means includes a corrugated metallic sheet.
 5. The apparatus as defined by claim 4 wherein the crest of said corrugated metallic sheet extended transversely of the longitudinal axis of said plenum and wherein said metallic sheet is perforated.
 6. The apparatus as defined by claim 1 wherein said third passage is disposed within said second spacial layer and wherein said partition has approximately the same length as said first and second elongated metallic plates whereby said third passage is separated from said first spacial layer; and second sealing means disposed within said second spacial layer extending transversely of the longitudinal axis of said plenum for sealing separating said second passage from said third passage.
 7. The apparatus as defined by claim 6 wherein said transfer passage is disposed intermediate said second inlet and said second sealing means with respect to said longitudinal axis.
 8. The apparatus as defined by claim 6 wherein said second inlet is disposed intermediate said transfer passage and said second sealing means with respect to said longitudinal axis.
 9. The apparatus as defined by claim 1 wherein said transfer passage extends through said partition.
 10. The apparatus as defined by claim 9 wherein said transfer passage is substantially the full width of said plenum.
 11. The apparatus as defined by claim 10 wherein said partition is comprised of two metallic plates disposed in end-to-end spaced relationship wherein the space therebetween defined defines said transfer passage. 12 The apparatus as defined by claim 9 wherein the longitudinal axis of said plenum is vertical; and wherein said transfer passage is disposed in the lOwer portion of said partition.
 13. The apparatus as defined by claim 12 wherein said second inlet to said second passage is s disposed below said transfer passage.
 14. The apparatus as defined by claim 12 wherein said inlet to said second passage is disposed above said transfer passage.
 15. The apparatus as defined by claim 1 including a third elongated metallic plate of generally similar peripheral configuration to said first and second elongated metallic plates contraposed in face-to-face spaced relationship with said second elongated metallic plate externally of said plenum; said first sealing means further sealingly connecting said second and third elongated metallic plates along the peripheral margins thereof whereby said third passage is defined therebetween; said first sealing means defining an inlet and an outlet respectively to and from said third passage.
 16. The apparatus as defined by claim 15 including a second partition within said plenum interleaved with said first partition and second elongated metallic plate whereby the opposing faces of said second passage are defined by said first and second partitions.
 17. A method of heat exchange including the steps of: providing a supply of gaseous phase heat exchange fluid; providing a supply of liquid phase heat exchange fluid; introducing the fluid of one of said phases into a first layer of a multilayer heat exchanger; distributing said introduced fluid of said one phase within said first layer substantially uniformly substantially across the width of said heat exchanger; passing the substantially uniformly distributed fluid of said one phase through the remainder of said first layer; simultaneously introducing the fluid of the other of said phases into a second layer adjacent said first layer; distributing said introduced fluid of said other phase within said second layer substantially uniformly substantially across the width of said heat exchanger; and transferring the substantially uniformly distributed fluid of said other phase from said second layer to said first layer while substantially maintaining its uniform distribution substantially across the width of said heat exchanger whereby the gaseous and liquid phases are substantially uniformly combined substantially across the width of a heat exchanger independently of their relative mass flows.
 18. A method of heat exchanging a first heat exchange fluid with a gaseous phase heat exchange fluid and liquid phase heat exchange fluid including the steps of: providing a first supply of liquid phase heat exchange fluid; providing a second supply of gaseous phase heat exchange fluid; providing a third supply of a third heat exchange fluid; introducing the fluid of one of said phases into a first layer of a multilayer heat exchanger; distributing said introduced fluid of said one phase within said first layer substantially uniformly substantially across the width of said heat exchanger; introducing the fluid of the other of said phases into a second layer adjacent said first layer; distributing said introduced fluid of said other phase within said second layer substantially uniformly substantially across the width of said heat exchanger; transferring the substantially uniformly distributed fluid of one of said phases from one of the first and second layers and diffusing it into the substantially uniformly distributed fluid of the other phase from the other of the first and second layers while substantially maintaining its uniform distribution substantially across the width of said heat exchanger whereby the gaseous and liquid phases are substantially uniformly combined substantially across the width of a heat exchanger independently of their relative mass flow rates; and passing the substantially uniformly distributed combined gaseous and liquid phase heat exchange fluids in heat exchange relation with said third heat exchange fluid.
 19. A method as defined by claim 18 wherein said one phase is the gaseous phase and said other phase is the liquid phase.
 20. A method as defined by claim 18 wherein said one phase is the liquid phase and said other phase is the gaseous phase.
 21. A method as defined by claim 18 wherein the combined gaseous and liquid phase fluids are passed generally upwardly through said other of said first and second layers.
 22. A method of operating a plate-type heat exchanger having a plurality of substantially parallel spaced plates defining therebetween a plurality of relatively thin but wide passages including the steps of: passing a gas into a first of said relatively thin but wide passages formed by said plates; spreading said gas out in said first passage over substantially the full width of said plates forming said first passage; passing a liquid into a second of said relatively thin but wide passages formed by said plates; spreading said liquid out in said second passage over substantially the full width of said plates forming said second passage; passing the thus spread gaseous and liquid fluids in substantially a common direction within their respective passages and passing one of said gaseous and liquid fluids beyond an edge of one of said plates forming one of a said first and second passages into the other of said gaseous and liquid fluids in the other of said passages for uniform intimate mixing of the gaseous and liquid fluids across the full width of said other passage; and passing the resulting mixture of gas and liquid in heat exchange relation via one of said plates with a third heat exchange fluid.
 23. A method of operating a plate-type heat exchanger having a plurality of substantially parallel spaced plates defining therebetween a plurality of relatively thin but wide passages including the steps of: passing a gas into a first of said relatively thin but wide passages formed by said plates; spreading said gas out in said first passage over substantially the full width of said plates forming said first passage; passing a liquid into a second of said relatively thin but wide passages formed by said plates; spreading a said liquid out in said second passage over substantially the full width of said plates forming said second passage; passing the thus spread gaseous and liquid fluids in substantially opposite directions within their respective passages and passing one of said gaseous and liquid fluids beyond an edge of one of said plates forming one of said first and second passages into the other of said gaseous and liquid fluids in the other of said passages for uniform intimate mixing of the gaseous and liquid fluids across the full width of said other passage; and passing the resulting mixture of gas and liquid in heat exchange relation via one of said plates with a third heat exchange fluid.
 24. A plate-type heat exchanger comprising: a plurality of substantially parallel closely spaced plates defining therebetween a plurality of relatively thin but wide passages; one of said plates being common to a first and second passage adjacent to each other; said one plate having an edge in fluid communication with each of said first and second passages; said first passage having a gas inlet; means within said first passage downstream of said edge for distributing gas entering said gas inlet uniformly across the width of said first passage; said second passage having a liquid inlet; means within said second passage downstream of said edge for distributing liquid entering said liquid inlet uniformly across the width of said second passage whereby said gaseous and liquid fluids are uniformly mixed as they pass beyond said edge of said one plate; and a third passage for conducting a third heat exchange fluid in heat exchange relation with the mixture of gas and liquid fluids. 25 The apparatus as defined by claim 24 wherein said edge extends transversely to said first passage.
 26. The apparatus as defined by claim 24 wherein said edge extends substantially across the full width of said first and second passages.
 27. The apparatus as defined by claim 24 wherein said edge is lower than said gas inlet to a said first passage.
 28. The apparatus as defined by claim 24 wherein said gas distributing means and said liquid distributing means abut opposite faces of said one plate.
 29. The apparatus as defined by claim 24 wherein said edge is the peripheral edge of said plate.
 30. The apparatus as defined by claim 29 including a second plate having a peripheral edge parallel to and spaced from said first edge, the space between said edges conducting one of said gaseous and liquid fluids into the other of said gaseous and liquid fluids.
 31. The apparatus ad as defined by claim 30 wherein said one plate and said second plate are coplanar.
 32. The apparatus as defined by claim 29 wherein said one plate and said second plate are noncoplanar. 